The gasification of coal to produce a methane-rich product gas is accomplished through the controlled slow heating of particulate coal in a gasifier comprising two or more zones, whereby any significant decrease in the density of the coal particles is minimized and particle swelling and friability are significantly reduced, while the carryover of fines and deposition of tars in the product gas conduit are thereby minimized. The particulate coal heating rate in the gasifier zones is usually between about 10° and 200° F per minute. When the particulate coal is to be fed to the gasifier at elevated temperature, further improvements are achieved with swelling type caking coals through their pretreatment by preheating the coal at a slow rate between 10° and 100° F per minute up to about 800° F in multiple fluidized beds. Any carryover of fines in the product gas stream from the uppermost zone of the gasifier is further reduced by utilizing either a solids separation step or a scrubbing step in the gas stream. The coal particles and/or tars thus recovered are returned to a high temperature zone of the gasifier.
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1. A process for gasifying particulate coal in a vertical multi-bed reactor comprising an upper bed, at least one (1) intermediate bed, and a lower gasifying bed, wherein the temperature profile of the reactor increases from the upper bed to the lower bed, and wherein an inventory of particulate coal is maintained in each bed, the coal being sequentially passed to each successively lower bed, comprising the steps of:
(a) passing particulate coal to the upper bed of the gasifier, the gasifier being maintained at a pressure between about 400 and 1500 psig; (b) passing a fluidizing gas comprising oxygen and steam upwardly through each bed of the gasifier at sufficient velocity to fluidize and heat each bed; (c) maintaining a heating rate of the coal in each bed of the gasifier at a rate between about 20° and 100° F per minute, whereby swelling and thermal disintegration of the particulate coal is minimized, (d) maintaining the coal inventory in the uppermost bed of the gasifier at a temperature between about 600° and 800° F; (e) transferring the coal from the upper bed to the next lower intermediate bed of the gasifier intermittently in batches, wherein the coal is heated to a temperature between 1000° and 1400° F thereby partially devolitilzing the coal, liberating tars and oils therefrom; (f) condensing the tars carried by the upwardly flowing fluidizing gases on the particulate coal inventory maintained in the upper bed of the gasifier, whereby the tars and oils are substantially hydrocracked upon sequential passage to the intermediate bed; (g) passing the partially devolitized coal to the lowest bed of the gasifier wherein the coal is heated to a temperature between about 1600° and 1800° F, such temperature not exceeding the ash softening point of the coal, whereby the coal reacts with the fluidizing gas thereby converting the coal into char, byproduct ash and a gaseous product; (h) removing a portion of the char and byproduct ash from the lowest bed of the gasifier; (i) removing a gaseous product stream from the upper bed of the gasifier.
9. A batchwise process for gasifying particulate coal in a vertical multizone countercurrent flow gasifier having at least three zones comprising an upper zone, at least one intermediate zone and a lower zone, the upper and intermediate zones having heat exchange means therein for maintaining a maximum temperature in each zone, the lower zone having a capacity to treat at least twice as much coal than in each of the upper and intermediate zones, comprising the sequential steps of:
(a) passing the particulate coal to the upper zone of the gasifier, wherein the coal is heated from ambient to a temperature between 600° and 800° F by the fluidizing gas, comprising oxygen and steam flowing upwardly through each zone of the gasifier at sufficient velocity to fluidize and heat the coal in each zone at a rate between 10° and 200° F per minute, whereby swelling and thermal disintegration of the particulate coal is minimized; (b) passing the heated coal from the upper most zone downwardly to an intermediate zone; (c) repeating step (a) thereby maintaining an inventory of fresh coal in the upper zone of the gasifier. (d) heating the coal in the intermediate zone to a temperature between 1000° and 1400° F, at a heating rate between 10° and 200° F per minute by the fluidizing gas moving upwardly through the gasifier, whereby the particulate coal is partially devolitized thereby liberating tars and oils; (e) passing the tars and oils upwardly through the gasifier to the upper zone substantially condensing the tars and oils on the coal in the upper zone; (f) passing the partially devolitilized coal from the intermediate zone to the lower most zone; (g) sequentially repeating steps (b) and (a). (h) heating the coal in the lowermost zone to a temperature between 1600° and 1800° F whereby the fluidizing gas moving upwardly therethrough reacts with the devolitized coal thereby producing a fuel gas; (i) removing at least one half of the coal inventory in the lower most zone; (j) sequentially repeating steps (f), (b) and (a); (k) recovering a gaseous product stream from the gasifier (l) removing by-product ash from the lowermost zone.
10. A process for the gasification of particulate caking type coal to produce a fuel gas, which comprises:
(a) feeding the coal into the top bed of a multiple bed pretreater at ambient temperature and atmospheric pressure; (b) passing a gas comprising less than about 1.0 SCF of oxygen per pound of coal upwardly through the beds of said pretreater to heat the fluidize and coal; (c) heating the coal in each bed of said pretreater at a rate between about 10° and 100° F per minute, whereby the swelling of the coal particles is minimized; (d) transferring said heated coal downwardly to the next lower bed of the pretreater intermittently in batches; (e) maintaining the temperature of said coal in the bottom bed of said pretreater at between about 600° to 800° F such that minimum devolatilization of the coal occurs; removing a gaseous product stream from said top bed of said pretreater. (f) feeding pretreated particulate coal from the bottom of said pretreater to the uppermost bed of a multibed gasifier; (g) passing fluidizing gas comprising oxygen and steam upwardly through the beds of said gasifier at sufficient velocity to fluidize and heat the beds; (h) heating the coal in each bed of said gasifier at a rate between about 20° and 100° F per minute; (i) maintaining the coal in said uppermost bed of said gasifier at a temperature between about 600° and 800° F by indirectly cooling the coal with an external fluid in heat exchange relationship with the bed; (j) transferring the coal downwardly to the next lower bed of said multibed gasifier intermittently in batches; (k) heating the coal in the next lower bed to 1000°-1400° F temperature whereby the coal is partially devolitilized thereby liberating tars and oils; (l) condensing the tars carried by the gases passing upwardly through said gasifier on the pretreated coal in the uppermost bed of said gasifier whereby said tars and oils are substantially hydrocracked upon passage to the next lower bed; (m) heating the coal in the lowest bed of said gasifier to between about 1600° and 1800° F such that the ash softening point of the coal is not exceeded and char is formed whereby the char reacts with the gas comprising steam and oxygen thereby converting the char into a gaseous product; (n) removing a portion of said char from the lowest bed of said gasifier so as to maintain an inventory of char in the bed; and (o) removing a gaseous product stream having reduced fines and tars from the uppermost bed of said gasifier (p) removing by-product ash from the lowermost bed of the gasifier.
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This present application is a continuation-in-part of copending U.S. patent application Ser. No. 365,910, now abandoned filed June 1, 1973, entitled "COAL GASIFICATION".
The gasification of particulate coal in a fluidized bed is known, having been disclosed by Garbo in U.S. Pat. Nos. 2,683,657 and 2,729,597, and by Forney in U.S. Pat. No. 3,463,623. In these patents, the particulate coal, on entering the gasification zone, is heated very quickly to the gasification temperature. Such rapid heating of the coal causes a decrease in coal density and also the coal particles structure is weakened. This results in the breaking up of coal particles in the gasifier to form low density fines. The decrease in coal density is a result of the coal particles undergoing swelling during the rapid heating. Such swelling is particularly noted in caking type coals. The swelling of caking coals upon heating has been studied and is referred to in "Some Relations in Rank and Rate of Heating to Carbonization Properties of Coal", J. S. Dulhunty and B. L. Harrison, Fuel, 32 (1953) at pages 441 et seq, and further in "Coal Typology -- Chemistry -- Physics -- Constitution", D. W. Van Krevelen, Elsevier Publishing Company, New York 1961, at pages 263 et seq.
In U.S. Pat. No. 2,131,702 Berry disclosed a process for making solid carbonized fuel, such as briquettes, from ground coal and a binder material utilizing very slow heating of the briquettes in non-fluidized beds with a hot non-reactive flue gas. This procedure minimized swelling of the briquettes and thereby maintained adequate strength and smooth surface during devolatilization.
Because of their low density, the hot fine coal particles are difficult to retain in the reaction zone when it is operated under fluidizing conditions. The result has been that a significant portion of the coal particle fines are carried out of the gasifier in the product gas stream along with some tars that are evolved during coal heating and gasification. This combination may cause plugging difficulties in the effluent conduits, resulting in frequent shutdowns of the process. Use of a longer free-fall section for heating the coal particles above the gasification zone has not been successful in overcoming such swelling and carryover problems. Although Jequier (U.S. Pat. No. 2,772,954) has disclosed a process for gasification of various type coals in multiple-beds, he utilizes continuous transfer of the particulate coal from the upper to lower beds, which involves quite rapid heating of the incoming coal particles to the average temperature of the coal in each bed. Furthermore, he operates his top bed at a sufficiently high temperature (500° C) to avoid the formation of tars therein.
The gasification of coal encounters added difficulties when caking type coals are used. The caking type coals tend to agglomerate as well as swell when subjected to the high temperatures employed in gasification, and cause handling problems.
Non-caking coals are of the anthracite and semianthracite types and caking or agglomerating coals are usually of the bituminous types described by the Committee on Chemical Utilization of Coal in "Chemistry of Coal Utilization", John Wiley & Sons, Inc., New York, Volume 1, 1945, pages 183 et seq and also by P. J. Wilson and J. H. Wells in "Coal, Coke and Coal Chemicals", Chemical Engineering Series, McGraw-Hill Book Company, Inc., New York 1950, pages 47 et seq.
Such problems in the gasification of various coals have made it difficult to develop a gasification process that can adequately handle the various types of coals, and especially the swelling type caking coals, to produce a clean fuel gas product.
It is an object of the present invention to provide a coal gasification process for producing fuel gas which may be operated for extended periods of time without substantial carryover of particle fines or deposition of tars in the gasifier outlet conduits.
It is another object of this invention to provide a coal gasification process wherein the coal particles are heated slowly in a multiple-zone gasifier to minimize swelling of the particles and to retain them in the gasifier, while condensing substantially all tars that are not liquid at ambient temperature on the coal particles in the uppermost zone of the gasifier. In the practice of the invention a process is employed for gasifying particulate coal in a multi-zone counter-current flow gasifier to produce a gaseous hydrocarbon fuel product. The coal enters the gasifier at a temperature between ambient and about 600° F where it is treated by contacting it in a low temperature first zone with a hot reactive gas stream from a second higher temperature zone while maintaining a coal heating rate in each heating zone at between about 10° and 200° F per minute to prevent substantial swelling and thermal disintegration of the coal particles during heating. After the coal has been further slowly heated to about 600° to 800° F, is past the heated particulate coal from the first zone to the adjacent second zone for further heating of the coal and hydrocracking of tars derived therefrom. In the intermediate zones, the coal is raised in temperature to about 1200° to 1600° F and thereafter treated by passing the heated particulate coal to a final gasification zone for high temperature gasification to produce a reactive heating gas. Hot gas containing tar vapor from the final gasification zone is passed countercurrent to the coal in the first and intermediate zones, whereby the tar evolved is substantially condensed and retained on the low temperature coal particles in the cooler zone. Char and ash by-product are recovered from the gasification zone and a fuel gas effluent product is recovered from the first zone.
It is a further object to provide a coal gasification process in which a multiple zone pretreater is combined with the gasifier to provide for the preferred overall slow heating of swelling-type caking coals from ambient temperature through pretreatment to a final gasification temperature of about 1800° F.
Other objects will be apparent from the description herein and the drawings.
FIG. 1 is a schematic drawing of an improved coal gasification system utilizing a multiple-zone pretreater and multi-zone gasifier shown in vertical cross-section view.
FIG. 2 is a schematic drawing of a similar coal gasification system wherein the product gas is scrubbed against a liquid to recover coal solids and tars for return to the gasifier.
In the present invention, particulate coal is heated to gasification temperature, e.g. about 1600°-1800° F, by a hot reactive gas to provide a controlled heating rate not exceeding about 200° F per minute, and usually between about 10° and 100° F per minute, and then gasified using an oxygen-containing gas to produce a methane-rich product gas. The gasifier used comprises two or more fluidized bed reaction zones, preferably three to five fluidized bed reaction zones connected in vertical series relationship and separated by a foraminous separator or perforated metal plate.
In a typical three-zone gasifier, the particulate coal is first heated slowly in the uppermost reaction zone to a temperature not exceeding about 800° F, and preferably about 600°-750° F, so that the tars released from the coal in the lower zones will be substantially condensed and retained on the coal within this uppermost zone. Such heating is provided by the hot reactive gases passing upwardly through the fluidized zones. After such controlled heating, the partially devolatized coal is transferred or dumped into an intermediate zone, wherein it is again slowly heated to a next higher temperature level and further devolatized by the hot reactive gases passing upwardly through the zone. The heated coal from the intermediate zone is then dumped into the lowermost zone for final heating and gasification.
In order to limit the swelling and friability of the coal particles, the heating rate of the coal particles in each pretreatment or intermediate zone should be about 10° to 200° F per minute, preferably about 20° to 100° F per minute. For the most economical results, the coal heating rate in the gasifier unit is about 20° to 50° F/minute.
A methane-rich product gas stream is withdrawn from the uppermost zone of the gasifier, while at least a portion of the resulting char and ash is withdrawn from the lowermost zone. The gasification process takes place at an elevated pressure range of at least about 100 psi, preferably between about 400 and about 1500 psig, and more preferably between about 600 and about 1000 psig so as to provide the product gas at commercially useful pressure levels.
It is also advantageous in the gasification of caking type coals if the particulate coal is first pretreated by heating it slowly from ambient temperature to at least about 500° and not exceeding about 800° F before the coal is passed to the gasifier. The use of such controlled slow heating rates in the pretreater further reduces the tendency of caking type coal particles to swell and break up in the fluidized zones, not only in the pretreater but also during subsequent processing in the gasifier. This pretreatment step is preferably used for caking type coals that usually swell appreciably on heating, although other coals could also be heated. Such controlled heating rate pretreatment preferably occurs in a fluidized multiple zone pretreater unit, with the coal being passed successively from the top zone to each lower zone while an O2 -containing gas is introduced into the bottom zone and a hot reactive gas is passed upwardly through the other zones. The controlled heating rates in the pretreater should be at least 10° F per minute and should not exceed 200° F per minute, while a rate not exceeding 100° F per minute is preferred and the optimum heating rate is between 15° and 40° F per minute. Those caking coals that swell the most would be heated at the 10° to 40° F per minute rate, while those caking coals with minimum swelling and the non-caking coals could be heated at the 100°-200° F per minute heating rate.
In order to further limit any undesirable coal fines and/or tars carried over in the product gas stream withdrawn from the uppermost zone of the gasifier, it is desirable to pass this gas stream through either a gas-solids separation step for the removal of particulate solids, or through a scrubber for the removal of both particulate solids and tars. The resulting solids-containing stream is then returned to the gasifier at a point below the uppermost zone, and preferably to its bottom zone. The coal solids thus recovered will usually comprise less than about 15% of the coal feed and preferably less than about 5% of the coal feed. If the product gas stream contains sufficient tar vapor to interfere with the proper operation of a centrifugal type solids separator, the gas stream can be passed instead to a scrubber unit and washed with either water or a light oil to remove the particulate solids and/or tar vapors. A cleaned gas stream is withdrawn off the top of the scrubber as product and a solids-containing liquid stream is withdrawn off the bottom of the scrubber and returned to the gasifier at a point below the top zone, and preferably to its bottom zone.
As shown in FIG. 1, a coal is fed to a preparation unit 10 where it is ground to a desired mesh size suitable for fluidization, preferably finer than about 8 mesh (U.S. Sieve Series) with a minimum size of about 325 mesh, and dried to remove surface moisture. The particulate coal is then passed through conduit 11 to the top of pretreater 12. The purpose of the pretreater is to heat the coal from ambient temperatures to a temperature at which minimum volatiles are being driven off, while at the same time approaching a temperature at which the coal particles will not be subject to excessive swelling when further heated for gasification. This is preferably accomplished by the controlled heating of the particulate coal in successive fluidized zones to about 500°-800° F in the presence of an upflowing oxygen-containing gas. The rate of heating should not exceed about 200° F per minute and preferably not exceed about 100° F per minute, while with caking coals that tend to swell it is most preferable that the heating rate be between about 15° and about 40° F per minute. Such slow heating also helps to minimize the reduction in the packed density of the coal particles.
The pretreater 12 can be operated at near atmospheric pressure using air as the source of oxygen in gas stream 16. The rate of heating in the top bed 14 can be further controlled by using a supplemental air stream (not shown). In such case of use of supplemental air, the gases in conduit 30 would preferably be burned as fuel. The pretreater can also be operated at the pressure of the gasifier 40 by using steam and oxygen as the gas in stream 16. In this latter case, the gases in 30 can be passed to the gasifier 40 or combined directly with product gas in 44.
The pretreater 12 in this embodiment comprises three fluidized beds of coal separated by perforated plates. The coal is first introduced into the top bed 14 at substantially ambient conditions of pressure and temperature, and is slowly heated therein to not over about 800° F and preferably to between about 600° and 700° F, with a hot gas introduced at 16 and containing some oxygen. The oxygen being supplied at 16 should not exceed about 1 SCF of O2 /lb of coal processed and preferably 0.4 to 0.7 SCF/lb of coal processed. More specifically, the coal is first introduced into the fluidized bed 14 where it is slowly heated to about 200° F by the upflowing gas passing through perforated plate 15. The heated coal is then passed via downcomer 18 and control valve 19 to the intermediate bed 20 for further heating therein under fluidized conditions maintained by the gas passing upwardly through perforated plate 21. Similarly, coal in bed 20 is heated slowly to an intermediate temperature of about 400° F and is then passed through downcomer 22 and control valve 23 to the bottom bed 26 for final heating therein to about 800° F by the gas passing upwardly through perforated plate 27. Only a portion of the pretreated coal is then withdrawn from the bottom bed 26. An inventory of pretreated coal should be maintained in the bottom bed 26 to provide for thermal balance between the exothermic endothermic reactions in the bed.
Gas is withdrawn from the pretreater at 30 and can be used as a fuel gas or can be further processed as desired. The coal heating rate achieved in these beds will depend upon the coal residence time in each bed, and the flow rate and oxygen content of the upflowing gas. Preferably, three to four fluidized beds should be used in the pretreater unit with the coal being slowly heated to the desired temperature in each bed and then dumped batchwise into the next lower bed.
Although the transfer of coal in the pretreater from the top bed to the lower beds has been shown and described as a preferred intermittent type process because of its greater degree of control, it is contemplated that for some types of coal having relatively low swelling characteristics the inter-bed transfer process may be made continuous. If the continuous transfer of coal is used, downcomers 18 and 22 would be extended to the upper surface of each respective fluidized bed to prevent the uncontrolled dumping of the coal in each bed to the bed immediately below. A continuous operation would of necessity require substantially more beds than a batch process to maintain the same slow average rate of heating.
After the coal has been pretreated by slow heating to between 600° to 800° F, it is withdrawn through valve 31 and passed through conduit 32 to storage bin 34 where it can be temporarily retained to provide adequate control of coal feed rates into the gasifier unit 40. The coal can be passed to weighing bins (not shown) and is then introduced by dense phase transport through conduit 38 into the uppermost zone of the multiple zone gasifier 40.
Gasifier reactor 40 comprises in this embodiment three fluidized beds arranged vertically in series and equipped with downcomer conduits having control valves therein suitable for transferring the hot particulate coal from the uppermost to the lowermost bed. Pressurized steam and oxygen are introduced at 42 into the lowermost bed where they serve to gasify the coal therein and resulting hot reactive gases pass upwardly through the fluidized beds located above. The oxygen content in stream 42 should preferably be such that the temperature in the bottom bed does not exceed the ash softening point of the coal, thereby facilitating removal of the resulting ash. Product gas is withdrawn off the top of the gasifier 40 through conduit 44. This gas may be subjected to subsequent separation for removal of any entrained oils or coal fines at 74 and may be further treated to provide a synthetic natural gas.
The particulate coal in uppermost bed 46 is fluidized by the gas passing upwardly through perforated separator plate 45 at sufficient velocity, at least about 0.2 ft/sec. superficial velocity. The temperature of coal bed 46 is controlled such that substantially all the tars in the rising gases that are not liquid at ambient temperature will condense and be retained on the coal particles therein. The temperature is controlled at between about 600° and 800° F preferably by a cooling fluid which passes through passageway 48 located in heat exchange relation with the fluidized bed 46. Such cooling fluid is usually water or steam, although other suitable fluids may be used. Control of the temperature in this uppermost bed to between 600° and 800° F also prevents tars from being evolved from the coal in this bed and passing out in the product gas through conduit 44 and depositing therein.
After the particulate coal has been heated in bed 46 at the desired rate and to the desired temperature, it passes through downcomer 50 via control valve 52 to intermediate bed 54 for further devolatilization therein at higher controlled temperature. Downcomer 50 preferably does not extend into bed 54 to facilitate the coal transfer. In bed 54, the coal is further heated to between about 1000° and about 1400° F by the hot gas passing upwardly through perforated plate 55. The temperature in bed 54 is preferably controlled by passing a suitable cooling fluid through passageway 56 located in heat exchange relation with the bed.
After the coal has been in intermediate bed 54 for a sufficient period of time to heat to the desired temperature and drive off the volatile matter that vaporizes at temperatures corresponding to the temperature of bed 54, the coal is then passed through downcomer 60 and control valve 62 to the lowermost bed 64 supported by perforated plate 65, for the final gasification at between about 1600° and about 1800° F temperature. Downcomer 60 preferably does not extend into bed 64 to facilitate transfer of the devolatilized coal. Structural parts of the lowermost high temperature bed may require cooling to maintain adequate mechanical strength.
Char and ash produced in lowermost bed 64 is withdrawn either periodically or continuously through conduit 66 and valve 68 to lock hopper 70, and then transferred at lower pressure to storage bin 72 where it may be cooled for further use. At least a partial inventory of char is maintained in bed 64 to maintain a balance between the exothermic and endothermic gasification reactions.
It is anticipated that the coal beds would be dumped sequentially commencing with the lowermost bed 64. Because a char inventory must be maintained in lowermost bed 64, this bed will therefore have a greater capacity than the beds above it. Ordinarily, the lowermost bed will hold about twice as much particulate material as the beds above and, therefore, about one half of the material in the lower bed will be dumped, thereby enabling the maintenance of a char inventory as described hereinabove. The bed next above the lowermost bed will then be completely dumped into the lower bed. This sequence will be followed until the upper bed is dumped and fresh particulate coal is passed into the upper bed.
It is preferred to transfer the particulate coal in each bed of the gasifier to the next lower bed intermittently on a batch-wise basis as hereinbefore described. However, the transfer valves and the number of beds may be so adjusted to permit the coal to be transferred to the next lower bed continuously if desired, particularly for coals having minimum swelling tendencies.
It is an important advantage of this invention that the rate at which the particulate coal is heated can be controlled from its initial temperature to the final gasification temperature. Such slow heating limits the thermal expansion of the coal particles, and thus serves to preserve their structural strength and density, particularly in the case of caking coals with observable swelling tendencies. Thus, the tendency for the coal particles to disintegrate in the fluidized beds to form low density fines is greatly reduced, with the result that substantially all the coal particles are retained within the gasifier beds until they are heated and gasified. Furthermore, by limiting the temperature in the uppermost bed of the gasifier to a level at which the tars evolved from the beds below are substantially condensed on the coal particles, such tars are then recirculated within the reactor for hydrocracking and are thus prevented from being carried into the exit conduits and deposited therein, thereby resulting in the gradual plugging of the conduits and shutdown of the process. Because the pretreated coal is somewhat porous, it can substantially absorb such tars without becoming sticky. Therefore, almost no material escapes from the gasifier having a boiling point above the controlled 600° to 800° F temperature of the uppermost bed. Such tars that do pass through the uppermost bed will usually be liquids at normal temperatures, so plugging in the outlet conduit 44 would not occur. However, the temperature of the uppermost bed should not be so low as to cause an accumulation of oils in the bed. Such control of the temperature in the uppermost bed also reduces the gas velocity at that point in the reactor, which further aids in reducing the carryover of fines into exit conduit 44. Also, the temperature of each bed except the lowermost should preferably be controlled such as by a cooling coil located therein or in heat exchange relation with the bed similar to the cooling coil 48 in bed 46.
Although only three beds have been described herein, the number of beds used in the gasifier is dependent upon the type of coal being gasified, the rate at which the heating of the coal is being controlled and the amount of coal being gasified. The temperature of the lowermost bed has been described as between 1600° and 1800° F, however, the final gasification temperature should usually not exceed the ash softening point for the coal being gasified in order to facilitate the removal of char and ash material. This temperature is controlled by the amount of oxygen in the gas entering the lower bed through conduit 42.
If the fluid used in cooling coil 48 in top bed 46 and cooling coil 56 in intermediate bed 54 is water, the resulting steam at 49 and 57 can be combined to provide at least a portion of the pressurized steam required at 42.
While the multiple bed type gasifier disclosed hereinbefore may be used for gasifying non-caking type coals without pretreatment to prevent swelling, its greater advantage and usefulness occurs when it is used on combination with the pretreater unit for processing caking type coals that swell upon heating. Furthermore, while it is preferred that the multiple bed gasifier be used with the multiple bed type pretreater as disclosed herein to provide for heating coal to about 600°-800° F at a slow rate, the gasifier may be used with other types of pretreaters which heat the coal at controlled rates.
Although this multiple-bed gasifier is effective in limiting the carryover of coal fines and tars in product gas stream 44, it is desirable under some conditions to obtain still further reduction of such carryover materials. Accordingly, as shown by FIG. 1, product gas stream 44 can be passed to gas-solids separator 74 for substantial removal of the particulate solids, and from which a cleaned product gas stream is withdrawn at 76. Separator 74 is preferably a centrifugal or cyclone type separator. A solids-containing stream is withdrawn at 78 and returned to gasifier 40. Stream 78 is preferably introduced into lowermost bed 64, at this permits reprocessing the recovered coal particulate solids through the entire multiple bed gasifier unit. Stream 78 is passed through a pressurizing means 80 such as a screw conveyor. If desired, pressurizing means 80 may comprise a venturi unit with gas-solids stream 78 being introduced into the throat section of the venturi, where it is mixed with and conveyed by pressurized gas stream 82. The solids in stream 78 will usually comprise less than about 15% of the coal feed rate and preferably less than about 5% of the coal feed.
If product gas stream 44 contains more tar vapor than desired in addition to some particulate coal solids so as to interfere with operation of centrifugal type separator 74, the stream 44 can be passed instead to a scrubber unit 86, as shown in FIG. 2. A scrubber liquid, comprising water or light hydrocarbon oil, is introduced at 88 and flows downwardly therein countercurrent with the rising gas. A cleaned gas product stream 90 is withdrawn off the top of the scrubber, and a solids-containing liquid stream 92 is withdrawn off the bottom. If stream 88 is water, the tar liquid will collect at an intermediate level in the scrubber unit 86, and can be withdrawn at 94. Slurry stream 92 containing some particulate coal solids, is returned to the gasifier unit 40 as previously described by action of pump 96. If the coal particles are not sufficiently wetted by water in stream 88 to provide for effective scrubbing and removal of coal solids from gas stream 90 in scrubber 86, a light hydrocarbon oil may be used as liquid stream 88 instead of water.
If desired, gas-solids separator 74 and scrubber unit 86 may be provided connected in series, so that the product gas stream passes first to the gas-solids separator and then to the scrubber.
Herein follow examples which set forth the application of the described process in the gasification of coal.
In order to show the effect of pretreatment on coal by slow heating in a fluidized multiple bed pretreater and show the effect of heating rate upon the packed density of the coal, two different grinds of Illinois No. 6 caking type bituminous coal are tested. Each sample is placed in a 2-inch diameter bed, surrounded by an electrically-heated furnace and the temperature is increased at selected rates to about 800° F while passing a gas containing a small percentage of oxygen upward through the sample to fluidize the particulate coal. Results for these samples are given in Table I.
| TABLE I |
| __________________________________________________________________________ |
| PRETREATMENT OF CAKING COALS |
| Run# 108/24 |
| 108/20 |
| 108/23 |
| 108/22 108/28 |
| 108/33 |
| COAL FEED 1 2 3 4 FEED 5 6 |
| __________________________________________________________________________ |
| Final Temperature,° F |
| 760 800 810 |
| 920 800 800 |
| Instantaneous |
| Avg. Heating Rate, ° F/Min. |
| 32 30 80 85 32 (> 200) |
| Pretreating Gas |
| V% Oxygen 10 10 10 10 10 2.5 |
| V% Nitrogen 90 90 90 90 90 97.5 |
| Supervicial Gas |
| Velocity, Feet/sec. 0.50 0.25 0.55 |
| 0.56 0.5 0.5 |
| Packed Density, g/cc 0.89 0.71 0.58 0.49 |
| 0.40 0.79 0.56 0.40 |
| Percent of Original Packed Density |
| 100 80 65 55 45 100 71 51 |
| Char Analyses After Heating |
| W% Ash 12.4 13.6 14.4 15.3 |
| -- 13.5 16.5 21.0 |
| W% Volatile Matter 39.6 30.3 23.1 25.4 |
| -- 40.2 22.9 22.8 |
| Particle Size: |
| U.S. Sieve - 20/50 23 27 32 33 -- 35 41 53 |
| - 50/100 56 55 54 53 |
| -- 54 47 43 |
| - 100/200 |
| - -200 21 18 14 14 -- 11 9 4 |
| __________________________________________________________________________ |
It is observed that the packed density of the pretreated coal particles decreases moderately upon heating to about 800° F at heating rates of 30° to 80° F/minute while exposed to the oxygen-containing fluidizing gas to produce similar devolatilization of the coal. Also, such packed density decreases further if the coal heating rates exceeds about 80° F/minute and if heated to above about 800° F temperature.
In order to show the effect on gasification of coal by slow heating in a fluidized multiple bed gasifier unit, samples of ground Illinois No. 6 coal are heated between specific temperature ranges at varying heating rates while passing an oxygen-containing gas upwardly through the fluidized coal samples. Each sample is placed in a 2-inch diameter bed surrounded by an electrically-heated furnace at an initial temperature, then heated to the higher temperature during a specific length of time, thus providing specific average heating rates. Results of these tests are presented in Table II.
| TABLE II |
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| Effect of Coal Heating On |
| Devolatilization And Gasification Of Coal |
| (105/25) |
| (105/26) |
| (105/18) (108/36) |
| (108/33) |
| (108/37) |
| (108/39) |
| Feed A B C Feed D E F G |
| __________________________________________________________________________ |
| Bed Initial Temp. ° F |
| 70 70 70 70 800 800 1600 |
| Bed Final Temp. ° F |
| 1200 1600 1600 1600* |
| 800 1600* |
| 1600* |
| Avg. heating Rate ° F/Min INSTANEOUS |
| Ambient - 800° F |
| 40 35 75 30 (>200) |
| (>200) |
| (>200) |
| 800-1200° F 14 25 45 20 -- 50 (>200) |
| 1200-1600° F |
| -- 20 20 14 -- 25 (>200) |
| Superficial Gas Velocity, fps |
| at 800° F 0.50 0.50 0.28 0.50 0.5 0.47 -- |
| at 1200° F 0.33 0.37 0.37 0.50 -- 0.42 -- |
| at 1600° F -- 0.46 0.46 0.46 -- 0.46 0.25 |
| Char Analysis W% |
| Ash 12.4 16.9 20.1 20.2 13.5 28.6 15.7 34.0 32.5 |
| Volatile Matter |
| 39.6 9.3 5.0 2.9 40.2 5.5 22.8 7.6 10.3 |
| Packed Density, g/cc |
| 0.89 0.60 0.61 0.50 0.79 0.44 0.40 0.30 0.27 |
| (Percent of Orig. Packed |
| 100 67 68 56 |
| Density) |
| Particle Size |
| U.S. Sieve + 50 |
| 23 31 27 31 35 41 53 36 30 |
| 50/100 56 53 51 59 54 40 43 42 48 |
| 100/200 |
| -200 21 16 22 10 11 19 4 22 22 |
| __________________________________________________________________________ |
| *Samples D, F and G were held at 1600° F temperature for |
| appreciable longer period of time than samples B and C. |
It is evident that the particulate coal samples being heated from ambient temperature to gasification temperature at slow heating rates, i.e., not exceeding about 40° F/minute, retains greater packed density than those being heated at more rapid rates. Also, the coal samples which are heated to final gasification temperature of 1600° F in multiple steps at slow heating rates (samples B, C, D) retain greater packed density than either that which is pretreated only by heating to 800° F at very rapid rate of 200° F/minute (sample E), or that which is pretreated at rapid heating rate and then further heated at a slow rate (sample F.) Furthermore, the coal sample which is both pretreated and then further heated at the very rapid heating rate (sample G) exhibits the greatest decrease in packed density of the coal particles.
Thus, coal heating rates used in the gasification temperature range are less critical than in the pretreating temperature range. While coal heating rates for pretreating up to about 800° F should be restricted to about 20°-80° F/minute, heating rates of about 30°-100° F/minute may be used for heating from about 600°-1200° F in the gasifier.
The carryover or elutriation of coal fines from a single bed pretreater connected in series with a single bed gasifier is compared to the carryover from a multiple bed pretreater and gasifier in accordance with this invention when operating at the same maximum temperature conditions. The results are set forth in Table III. The results are based on 1270 lb/hr. dry coal feed to the pretreater and 1000 lb/hr. pretreated coal fed to the gasifier.
| TABLE III |
| ______________________________________ |
| Single Bed System |
| Multiple Bed System |
| Pretreater |
| Gasifier Pretreater |
| Gasifier |
| ______________________________________ |
| Pressure, psig |
| 400 400 400 400 |
| Temperature, ° F |
| 800 1800 800 1800 |
| (Max.) |
| Superficial |
| Upward |
| Gas Velocity, fps |
| 0.6 0.4 0.6 0.4 |
| Coal Elutriation |
| Rate lbs/hr. |
| -- 203 1 7.5 |
| Coal Elutriation |
| Rate W% of feed 20.3 0.1 0.8 |
| ______________________________________ |
It is seen that the coal particle elutriation rate from the pretreater is negligible, while that from the single bed gasifier is 20.3 wt. percent of feed, as compared with only about 0.8 wt. percent of feed for the multiple bed gasifier.
Although various specific embodiments of the invention have been described and shown, it is to be understood that they are meant to be illustrative only and not limiting. Certain features may be changed without departing from the spirit or essence of the invention. It is apparent that the present invention has broad application to the gasification of caking and noncaking coals. Accordingly, the invention is not to be construed as limited to the specific embodiments illustrated but only as defined in the following claims.
Shen, John, Johnson, Clarence A.
| Patent | Priority | Assignee | Title |
| 10766059, | Mar 25 2016 | ThermoChem Recovery International, Inc. | System and method for recovering inert feedstock contaminants from municipal solid waste during gasification |
| 10946423, | Mar 25 2016 | ThermoChem Recovery International, Inc. | Particulate classification vessel having gas distributor valve for recovering contaminants from bed material |
| 11242988, | Feb 16 2016 | THERMOCHEM RECOVERY INTERNATIONAL, INC | Two-stage energy-integrated product gas generation system and method |
| 4308668, | Jun 04 1979 | Mitsubishi Jukogyo Kabushiki Kaisha | Process for heat treatment of coal |
| 4474583, | Jun 11 1982 | FOSTER WHEELER ENERGY CORPORATION, A CORP OF N J | Process for gasifying solid carbonaceous fuels |
| 4621952, | Jul 28 1981 | UNION CARBIDE CORPORATION, A NY CORP | Fluidized bed discharge process |
| 4636300, | Sep 13 1984 | RUHRKOHL AKTIENGESELLSCHAFT | Integrated gas-phase hydrogenation process using heat recovered from sump-phase hydrogenation for temperature regulation |
| 4696735, | Oct 20 1984 | Ruhrkohle Aktiengesellschaft | Method and apparatus for multiphase coal hydrogenation reactors with exothermal heat of reaction having gas cooling in sump-phase reactors |
| 5634950, | Feb 24 1994 | THE BABCOCK & WILCOX POWER GENERATION GROUP, INC | Black liquor gasifier |
| 6117199, | Apr 26 1982 | Foster Wheeler Energia Oy | Method and apparatus for gasifying solid carbonaceous material |
| 8808972, | Apr 15 2004 | Ushio Denki Kabushiki Kaisha | Optical films and methods of making the same |
| 9464245, | Nov 01 2010 | PROCESS ENGINEERING, CHINESE ACADEMY OF SCIENCES | Apparatus and method for multistage hierarchical pyrolysis and gasification of solid fuels |
| Patent | Priority | Assignee | Title |
| 2131702, | |||
| 2579397, | |||
| 2588076, | |||
| 2591595, | |||
| 2633416, | |||
| 2683657, | |||
| 2772954, | |||
| 3740204, | |||
| 3746522, | |||
| 3817723, |
| Executed on | Assignor | Assignee | Conveyance | Frame | Reel | Doc |
| Jun 10 1975 | Hydrocarbon Research, Inc. | (assignment on the face of the patent) | / | |||
| Mar 31 1983 | HYDROCARBON RESEARCH, INC | HRI, INC , A DE CORP | ASSIGNMENT OF ASSIGNORS INTEREST | 004180 | /0621 | |
| Jan 24 1994 | HRI, INC | HYDROCARBON RESEARCH,INC | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 006847 | /0641 | |
| Jan 31 1995 | HYDROCARBON RESEARCH, INC | Institut Francais du Petrole | ASSIGNMENT OF ASSIGNORS INTEREST SEE DOCUMENT FOR DETAILS | 007662 | /0308 |
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